Of san francisco



Dec. 20, 1927.

R. w. HANNA ET AL.

DISTILLATION OF PETROLEUM OIQS F'led Oct. 2, 1922 3 Sheets-Sheet l Maf@ Ewdmbu ich N www Dec. 20, 1927. 1,653,431

R. w. HANNA ET AL DISTILLATION oF PETROLEUM oILs Filed 061.2, 1922 s sheets-sheet 2 Qu Maut .5u uk Lim: 32522K Dec. 20, 1927. 1,653,431

R. w. HANNA ET AL,

DISTILLATION OF PETROLEUM OILS Filed Oct. 2, 1922 3 Sheets-Sheet 3 Cil Patented Dec. 20, 1927.

UNITED STATES PATENT OFFICE.

RL'CHARD XV. HANNA, 0F PIEDMONT, AND RICHARD Cl'. HANNA, OF BURLINGAME, CALI- FORNIA, ASSIGNORS, BY MESNE ASSIGNMENTS, TO STANDARD OIL COMPANY OF GALTFORNIA, OF SAN FRANCISCO, CALIFORNIA, A CORPORATTON OF DELAWARE.

DISTILLATION OF PETROLEUM OILS.

Application filed October 2, 1922.

This invention relates primarily to the art of distillingl crude petroleum, although certain aspects ot the invention may be effectively utilized in connection with destructive distillation thereof. commonly known as cracking, and in other aspects the invention ma),Y be applied in re-dstillation ol distillates produced other distillations.

In one ot its aspects this invention comprehends the process and apparatus tor the continuous production. from crude petroleum. ot distillates having the desired boilingpoint ranges so that re-distillation will not be required.

ln another aspect this invention comprehends the continuous production 'from crude petroleum ot' distillates having` the desired boiling.r point ranges so that not only will redistillation be unnecessary but the desired products will be obtained. one trom each distillinoA unit. in such a way that mixing or blending` will be unnecessary, and at the same time a maximum practical yield of the desired distillate will be obtained.

In another aspect this invention comprehends the continuous production ot any dosired number ol distillatos o't' various boiling point ranges by using a number. corresponding' to such desired number ot' distillales. ot distilling units pioperly opcatively connected together.

lit is understood that various attempts have been made to liuoiilucc distillates from crude petroleum which will require no redif-tillrtion Some ot those have been by Fractional distillation and Sonie by 'tractional coi'idensation, wherein the rctluxes from Ylractiomil condenser or troni various points in a Ytrzutionatinof column are diverted as the desired products. However. so tar as is known. no eipiipment or process has been developed which has ma de it possible to produce troni a single still a single distillate with the boiling point range such thatneither re-distillation nor blending with other distillate-s would be. necessary.

in order to accomplish these results it has leen 'found that lirst ot all it was necessary to develop a means Vtor the accurate and positive control ot the heat dissipation from the vapors evolved in the distilling` unit so that br ns control the necessary reflux can be obtained and the desired distillate pro- Serial No. 591,773.

duced. lt has further been found that to produce the desired distillate the temperaturcs ot the vapors to be condensed must be accurately controlled and this regardless of disturbing intl uences within the system, such as the rate ot tiring. still temperature, or changes in the character ot or rate of feeding` the crude.

It has been tui-ther tound that net only is it necessary to have the distillate Vapor temperatures within the control of the operato: s. but tor ellicient operation it is necessar;v to malte use ot a tower wherein the evolved vapors may be thoroughly scrubbed by descending reflux oils before entering the temperature control chamber.

lriel'ly a preferred embodiment of the invention in a process and apparatus may be described as i'ollows:

The crude oil is ted into a. tower connected to a :till: in connection with the tower is a heat dissipation (or distillate temperature control) member, suitable condensing equipment and desired heat exchanger. The evolved vapors pass from the still to the tower where they are contacted with the incoming Ytred and the descending reflux and where the desired scrubbing takes place, thc 'lced and retin); running to the still and the contacted vapors passingto the reflux control member. where the heat dissipated, (and thus the reflux.) is so controlled that only vapor existing at a determined ten'iperaturc remains. The residue distillate vapors then are emitted `l'rom this control chambmV at the determined temperature and pass on to bc condensed asdis'tillates requiring no further distilling. `Wlien it is desired t0 produce more than one cut from the crude petroleum. the residuum 'trom the tirst still is carried to a second distilling;V unit and a second cut produced. This process may be repeated tor any desired number of cuts.

While this invention is most Valuable in the production ot' tinisbed boiling point distillates directly trom crude petroleum it is readilyY understood that because of the nature ot the process and equipment any petroleum oil containing` the desired fractions can be successfully tractioned by use of this invention and the use of the invention for the production oit desired distillates from any petroleum oils is comprehended. We

Fig. 3 is o diegroininmiii vien' illuetraiting two units Coupled in series.

Fie; el a side elevation el" another form of epporetus.

ln Fig. 1 olf the droifinrf.: indicates e. still which ie preferably divided into o Se ries oit' coinpertinente by rin-tical partitions S. .lu the drenfingl's these pertiiions 3 .fire ini dieifited welded to the inner sur'lfuce of the still il. so :is to forni iuui-coinnuinieating colui orlnieubs in the still. The still 2 indicated es .uioruited oi'er u suitable 'fur-noce l heeled by the con'ibustion oit fuel troni e euituble burner 5. ,Frein the inlet Compartment 6 u pipe l extends upward from neer tbe bottoni el? the compartment und thence through the partition. 3 opening into the udjoining` compartment o. Conii'nunieetion between the other adjacent coinpriirtuients is by ineens of" siniilini iii-pee 7. 11 indicates Vapor .lines leading kfrom tle respeetive Comparo niente und discharging into ai common vapor line or houder ln the oifperatus thus ill strolled, the W'tlidrou'el of evolved Vu.- pors from the respective compartments in'- deijieudent olf the other coinimrtuients. rlfhe vwoor line or heeder 12 preferably inelines slightly duo-"NunT l liowurd and enters into `the tower 13 sliehlil'v above 'the bottoni.. The

or tzu' heut exchuneer 1"? und thenee into the tower 18 intermediate its ends. Prefemblifthe incoming oil is delivered by the leed pipe lll; onto one of the baille plates. E indientes u. vapor line 'from the top of the tower 13 eni'zerino; `lrhe regulable heat diseipution member 15) preferably u short distance Vabove the bottom thereof ond et the side of reeeuei member 19 sothat communication from the chamber 21 to the chamber il?. is through these tubee ln the Vapor chamber oi. the nieiuher 19 (between the tube-sheets 9.0) deflection pluies ure provided so thut vapors entering the churnber frein l'he 'vapor line 18 are caused to circulate beck und forth through the chamber in passing upward therethrough, thus contacting repeetedly with the surfaces of the tubes 23, .finally passing' out through the Vapor outlet 25 into Vhe liue 26 which in turn pueses through the .opor heat exchanger 16, und thence through u continimlyioi: ol the line Q6 tl'u'ough the cmidenffu il?. und 'from thence to Suitable storage. QS indicatori u. vulve upon this con deueule line. 'lhieI vulve, in the use of 'the 'torio ol oppurutus shown iu Fig. 1, is noriuullj.' open. 2f) indicates u. conduit for the (,lruu'iny; oil ol the condensate i'irointhe mene bei. 1) :uid discharging.; such condensate into the 'tower 13 at the top thereo'li. Where it is showered onto. und into the uprising vapors. indicated in ig'. 3 'this line 29 enters into pou 30 which :forms u seul or trop of condensate. preventing the uinising;v vapors entering the reflux line 29. lt is obvious that un): prueticul liquid trop, such :for initunce es .hewn in Fie'. 4l, muy be used. .lli to be noled tl'iiit the mp line 155 entere die .member 19 efbove the i ,el oli lli-e reflux draw oil line 29. 31 iudieet :i .line from the l.o\\'- er 13 to the first cornpiirliuenl: olf the still. Wherebjifthe reflui: mid inconnue; leed prei'- erebly posses onto :i suitable distributing pun 32 oil the ordinary or any preferred eon struction.

indice :i reeiduel oil the i uif'ention is perfo retus consisting einiipl'y of one producingln onlyv one :'llute. then the ed line o@ oo eoniniurneu-.es with the compartnient 109 or hottest purl; o'l the still und carries the resilual oil to lue heut exehunger 17 und to end through the cooler l lroin this the cooled residual oil or lier passed by the line 35 to suitable storage. llvlhen, hou Avr. the upporutus e. iu the 'lfm-in of ay series olz mlm-communicoting Stills t2? (es indicated. in Fig'. then. the liue 33 is' connected by n eniis of o suitable iru'fnip Sli lio the feed line 14. of the neil; Still. The Withdrawal et residrml oil or tur iiroin the lest still oi :i series or bitter;` "Wohle referulili,T be that indicated in Figi'. .1. VWhile hief. il indiezutes the arrangement el the ri'iilufieuul of residual oil from one still and its feed into a subsequent still of the battery.

3T indicates aI steam line leading'from a suitable supply. From this line 3T lines 38 provided with suitable valves -l9 lead to nearly the bottom of the still where the steam is discharged into the respective coinpartments of the still through perforated yhorizontal pipes 39.

et() indicates a draw ott from the still there may be provided a similar draw otl` from each compartment it desired. -ll indicates a water line leading` from any suitable source of supply and connected through the pump 42, valve 42 and line 43 to the chamber 21 of the member 19. fi-i indicates a steam line leading from the chamber 22 for discharging the steam evolved in the member 19. lt is obvious that if desired chamber 22 may be connected with the line 37 by means of suitabie regulating devices. 45 indicates a temperature indicating device, suitably connected with a temperature measuring device 4G in the vapor line 2G. 47 indicates a suitable temperatureindicating device connected with a suitable temperature measuring device 118 in the compartment 10 of the still it desired there may be similar indicating and measuring devices for each of the con'ipartments.

In Fig. 4t the still 2 is indicated as an ordinary steam still provided with a steam supply line 3T connected with a distributing pipe 39. This still may or may not be mounted over a suitable furnace as desired. As shown in Fig. 4 the feed line 1-1 passes through vapor heat exchanger 16 and thence into the tower 13 intermediate its end. 12 indicates the vapor line from the still Q to the tower 1? and 31 the re'tlux line -trom the bottom of the tower 13 to the inlet end of the still The vapor line 1S from the tower 13, regulable heat-dissipating member 19.` reflux line 29 trom the member 19 to the tower 13, vapor line 26 from the member 19 to the heat exchanger lli' to a suitable condenser 27 all correspond with similar devices of Fig. 1. In Fig. et the reflux line 29 is shown with a trap form-ed by the low bend of the line providing a liquid seal against vapors of the tower lil passing upward through this line 29.

In order to counteract any changes in temperature conditions due to changes of weather, and retain the heat dissipation within the regulable control of the operator, all of the apparatus from the still 2 to the entrance of the condenser 2T is suitably insulated to prevent the dissipation of heat. This insulation is not specilically indicated in the drawings. It, however, may consist of asbestos sheets and plaster properly applied. or of any other suitable or preferred heatinsulation.

Preferably water or other liquid is fed to the chamber 2l of the heat dissipatiug member 19 at such a.. rate as to compensate for evaporation losses and to maintain such a level in the member 19 that the correct amount of effective cooling surface will be in contact with vapors so as to bring about the desired temperature of the distillate vapors. The fractions condensed from the vapors because of the resultant reduction of temperature are those not desired in the linal product and are returned to the tower as reflux. This regulation may be accomplished by varying the llow ot cooling medium to such chamber by anyv suitable means such as the valve control indicated in the drawings. The temperature indicating de-. vices' make possible the observation of the distillate vapor temperature. lVith this method ot' control a constant pressure is lneferably maintained on the cooling medium within such member by opening directly to the atmosphere or by means of valves or other suitable devi'ccs. There water is used as the cooling medium, more or less violent evaporation of the same takes place became of the high vapor temperatures. ln case other cooling medium be furnished to the chamber 21, such for instance as an oil of such characteristics that little evaporation takes place under the iinpesed conditions of pressure and temperature, the quantity of such cooling medium admitted and the quantity withdrawn is suitably controlled by valves or other usual means so as to maintain just sulticient cooling medium within the member 19 to efl'ect the desired heat dissipation.

lt is recognized thatby correct design of the member 19, it is possible to ellect the coi'- rect dissipation of heat by iiowing a. liquid through the entire cooling' surface of said member and vary the coolingeiiiector dissipation of heat by varying the rate or temperature ol the cooling medium passingr therethrough.

The condensate from the member 19 passes down to the tower wherein it is scrubbed against up-coining vapors. lt should be noted that in this part of the tower the up coming vapors are in contact only with a condensate of said vapors and thereby a thorough sifting of the lighter fractions from the heavier is obtained. At a point lower in the tower the feed line enters and the feed to the distilling unit is introduced against the tip-coming vapors. ln this portion of the tower a rough scrubbing of the tip-coming vapors occurs in which the vapors, reiuX, and feed oil are brought to substantially the same temperature. It will thus be seen that by bringing1 the feed stock to be distilled into the vapor tower at a point intermediate its ends. and bringing the reflux from the heat dissipation member into the vapor tower at its top, there is provided a three stage liu) succeeding; distillate mada 4, ncaaaai.

separation or condensation. By this means a much more thorough sitting;v ot the heavier or higher boiling point' fractions from the evolved vapors is attained than has heretofore been possible ivithout re-distillation it has also been found that by the use ot' the controllable heat dissipation ot the evolved vapors, as Well asy by this three stage .retluxing, a higher percentage ot those ractions with boiling points ivi'lh'iu the desired range is obtained than by any hitherto known method. This advantage ot incroasing the yield of the lirst distillate also has a marked beneficialv e'lect upon 'the subsequent distillate Where a plurality of stills are operated together as indicated in Fim. 8, and When the second distillate is desired to have what is commonly lrnoun as a relatively high flash point. "l, iis advantao'e inurcs to each Where series dis tillation is carried out j'brouggli a plurality of distillinp; units by pa sind the residual oil vtrom one .distilliiv4 unit u another and operating all such un, in at ordance with this embodiment ot the invention. rthis advantage probably due to the shorteninp of the overlap oit the end pointel oit the respective distillates.

By the proper control ot the it'eod ot cooling medium to the chamber 2l. ot the incinber 19, the eiliiective coiulensingl sini'ace ot the member lll may be varied as required .in the operation. This enables thc operator to control the temperature ot the discharged vapors so that such temperature may be so maintained as to produce a distillate oit the desired boiling point range, even where the rate ot distillation varies or where other tactors eli'ecting; the evolution ot vapors troni the distilling operation occur.

By thus providing` regulable control. oi the heat dissipation, the operator can control the boiling point range or lgravity of the distillate produced subst:initially independent ot the increase or decrease ol' the heat supplied to the oil for distillation and may suitably control suchv output independent ol the rate of distillation.

1We claim:

l. A process of ,distilling petroleum oil, which consists in continuously distilling an oil, cpntinually passing the evolved vapors to a vapor tower, continuously passing the evolved vapors -trom said toiver to a heat `dissi atina member and there hrine'ine' the D di? vapors to a desired discharge temperature by dissipation ot heat troni the vapors to a liquid cooling medium the temperature oit which is controlled Without varyingn the character oit' the 'feed to the tourer, continucontinuously returning tire eoiidensate troni Y such dissipating` member to said toiver, continuously supplyingthe ,oil to he distilled vapors are scrubbed by the toed oil to thel system, together with a condensate trom the other stages, in the second stage are scrubbed a. inist the condensate Ytrom the third stage,

`and in the third stage are brought to a de aired discharge temperature by controllably dissipating the heat thereof to a separately regulated cooling` medium the 4temperature ot Which is controlled Without varying the character ot the feed oil, condensingas one product the vapors 'from said `third stage, and passing; `the condensate trom such vapor separatinp` system together ivith the toed oil to the source ot' evolved vapors, said process being characterized by the separation of no intermediate product.

i3. The' process ot continuously distilling petroleum oil, Which comprises continuously raporizing an oil, continuously passing the vapor through a three stage vapor separatingr system, in the first stao'e ot which the vapors are scrubhbed against the 'leed oil to the system together with the condensate 'trom the other stages, in the second stage ot which the vapors are altered only by the scrubbing action ot the condensate trom the third stage, and in the third stage the vapors are brought to a desired discharge teniperature by coiitrollably dissipating the heat thoreot to a separately regulated liquid coolii'ron medium the teinperatiu'e oi vvhich is controller; .vithout varying' the character of the feed oil, condensing: as one product the vapors from such third stage., and passingF the condensate trom said vapor separatnfig` systen'i together with the teed oil to the source ot the evolved vapors,y said process being` characterized by the separation ot no intermediate product.

4. fr process ot distillingr petroleum oil comprising; continuously vaporizinrg an oil, continuously passing the evolved vapors through a vapor separating; system vvherein the vapors are progressively subjected to Erst the scrubbing action ol the condensate from the other stages oit the system and the 'feed oil to the system, and are last brought to the desired discharge temperature by dissipation of heat from such vapors to an in dependently' regulated cooling medium the temperature ot which is controlled Without varying1 the character ot the feed oil, the feed oil together Wit-h the condensate troni said system being continuously passed to the source the vapors, and continuously con i lll""lllllllllllll densing as one product the vapors from said vapor separating system, the cooling inediuni being maintained continuously in the boiling` condition, said process being characterized by the separation of no ii'iterinediate product. 5. A process of coutiuuourslr distilliug a petroleum oil comprising eontmuousl)y ond stage ot' which the vapors are subjected only to't-he condensingI action oi" the condensate 'from the third stage. and in the third stage the vapors are brought to a desired discharge temperature by controllably dissipating` heatl thereotl to a separate liquid cooling` inediuin the temperature of Which iS controlled without varying the character of the feed oil maintained at its boiling point, the feed oil together with the condensate from such vapor separating system being passed to the source of evolved vapors, and condensingl as one product the vapors from such Vapor separating` system, said process being characterized by the separation of no intermediate product.

Signed at Richmond, Calif., this 22nd day of September, 1922.

RICHARD XV. HANNA.

RCHARD JA. HANNA. 

